Process for the manufacture of industrial and power gases



Oct. 10; 1950 M. STEINSCHLAEGER PROCESS FOR THE MANUFACTURE OFINDUSTRIAL AND POWER GASES 8 Sheets-Sheet 1 Filed June 10, 1944 wm xxx12; m iix x X x x K x x W x x w md axxvai x 8 Sheets-Sheet. 2

M. STEINSCHLAEGER PROCESS FOR THE MANUFACTURE OF INDUSTRIAL AND POWERGASES Oct. 10, 1950 Filed June 10, 1944 Oct. 10, 1950 M. STEINSCHLAEGER2,524,349

PROCESS FOR THE MANUFACTURE OF INDUSTRIAL AND POWER GASES Filed June 10,1.944 8 Sheets-Sheet 3 Oct. 10, 1950 M. STEINSCHLAEGER 2,524,849

PROCESS FOR THE MANUFACTURE OF INDUSTRIAL AND POWER GASES 8 Sheets-Sheet4 Filed June 10, 1944 Oct. '10, 1950 M. STEINSCHLAEGER 2,524,349

mocmss FOR THE umumc-rg ag or INDUSTRIAL AND POWER G 8 Sheets-Sheet 5Filed June 10, 1944 i c Iii 1'02 71 w W (a r-i Oct. 10, 1950 M.STEINSCHLAEGER PROCESS FOR THE MANUFACTURE OF INDUSTRIAL AND POWER GASESFiled June 10, 1944 8 Sheets-Sheet 6 a a 100* 400 f? j a z A I w 149 4 Lw 1&2

lad/9 Oct. 10, 1950 M. STEINSCHLAEGER 2,524,849

PROCESS FOR THE MANUFACTURE OF mnusmm. mo POWER GASES Filed June 10,1944 a Sheets-Sheet v Q $1 Tvg xvi Oct. 10, 1950 M. STElNSCHLAEGERPROCESS FOR ma MANUFACTURE OF mnus'mm. AND POWER GASES 8 Sheets-Sheet 8Filed June 19, 1944 Patented Oct. 10, 1950 PROCESS FOR THE MANUFACTUREOF INDUSTRIAL AND POWER GASES Michael Steinschlaeger, London, England 1Application June 10, 1944, Serial No. 539,686

In Great Britain July 28, 1943 t 3 Claims. This invention relates to themanufacture of water gas and other industrial and power gases. v'I'heinvention is concerned with a process of gas-making which isadvantageously carried out with improved arrangements of apparatuscomprising or consisting of a generator provided with a grate,preferably an automatically operated grate.

The term generator as used herein includes a producer.

When using a generator provided with an automatically operated gratedifllculties sometimes arise owing to the grate being subjected to toohigh temperatures which render it necessary to renew the grate at fairlyfrequent intervals. Attempts have been made to overcome this difficultyby providing a jacket boiler around the generator but this has thedisadvantage of increasing the fuel consumption.

It is an object of the present invention to overcome this disadvantage.

It is a further object of the invention to provide an improvedintermittent gas-making process carried out in a generator of the gratetype without resort to a jacket boiler or similar means for withdrawingheat from the vicinity of the grate and in which the thermal efllciencyof the process is improved by recovery and re-use in the process of alarge part of the heat that would otherwise be carried out of thegenerator in the ash or in the cooling water when a similar jacketboiler or similar means has heretofore been employed.

- It is a still further object of the invention to provide an improvedapparatus including a generator with or without a regenerator suitablefor use in the manufacture of all kinds of industrial and power gases,for example blue water gas, carburetted water gas and synthesis gases orgases containing hydrocarbons such as benzene, toluene, butadiene orother olefines, in a satisfactory and economical manner.

With these objects in view the present invention provides a process forthe manufacture of water gas and other industrial and power gasesemploying a generator provided with a grate, preferably an automaticallyoperated grate, one or more conduits disposed above the grate and in thelower half of the generator for the introduction or removal of fluids,one or more conduits disposed below the grate for the admission orremoval of gases or vapours used for the reactions and one or moreconduits in the upper part of the generator and at least 55% of theheight 'of the generator above the bottom thereof, for the introductionor removal of fluids.

The present invention also provides an apparatus for the manufacture ofindustrial and power gases which comprises a generator provided with agrate, preferably an automatically operated grate; a reaction zone ofincandescent fuel, one or more conduits disposed above the grate andbelow the bottom of the reaction zone, for introduction and removal offluids, one or more conduits disposed below the grate, for the admissionor removal of gases or vapours used for the reactions, and one or moreconduits at or above the top of the reaction zone for the introductionor removal of fluids.

Furthermore, the apparatus preferably includes a regenerator which isconnected to the generator, for example by a conduit joining a point ator near the top or the bottom of the generator and a point at or nearthe top or the bottom of the regenerator.

Itwill be understood thatthe apparatus according to the invention willinclude means for introducing fuel into the generator and removal of ashand valves necessary for controlling the flow of fluids through thegenerator and regenerator and may also include conduits additional tothose mentioned above.

A few embodiments of the invention will no he described by way ofexample with reference to the accompanying diagrammatic drawings, inwhich like parts are indicated by like reference characters. and inwhich:

Fig. 1 is a diagrammatic drawing of an apparatus according to theinvention suitable for the manufacture of blue water gas;

Fig. 2 is a similar drawing of an apparatus suitable for the manufactureof carburetted water Fig. 3 is a simflar drawing of an apparatussuitable for the manufacture of synthesis gas;

Fig. 4 is a similar drawing of a simplified apparatus consisting of agenerator only for the manufacture of blue water gas;

Fig. 5 is a similar drawing of a simplified apparatus consisting of agenerator only for the manufacture of carburetted water gas;

Fig. 6 is a similar drawing of a simplified apparatus consisting of agenerator only for the manufacture of synthesis gas; 7

Fig. '7 is a similar drawing of an apparatus consisting of a, generatorand two superheaters for the manufacture of carburetted water gas;

Fig. 8 is a similar drawing of an apparatus consist ng of a generatorand a su rheater for the manufacture of carbmetted water gas:

Fig. 9 is a similar drawing 01 an apparatus consisting of a generatorand a regenerator di- 'vided into two parts for the manufacture ofcarburetted water gas;

Fig. 10 is a similar drawing of a modification of the apparatus shown inFig. 9;

Fig. 11 is a similar drawing of an apparatus consisting of a producerand a regenerator for the manufacture of producer gas;

Fig. 12 is a similar drawing of an apparatus consisting of a generatorand regenerator for the manufacture of carburetted water gas;

Fig. 13 is a similar drawing of an apparatus consisting of a generatorand two regenerators for the manufacture of synthesis gas, and

Fig. 14 is a similar drawing of an apparatus consisting of a generatorand two regenerators, also for the manufacture of synthesis gas.

Referring to Fig. 1 of the drawings, the generator I has anautomatically operated grate 2. The reaction zone is indicated by thenumeral la, the portion of the fuel bed above the reaction zone by thenumeral lb and the ash bed by the numeral lc.

The generator is provided with conduits 3, 4, 5, 6, I, 8, 9, i and H,controlled respectively by valves 3a, 4a, 5a, 6a, Ia, 8a, 9a, lfla andHa. The generator is joined to the regenerator I2 by the conduit l3controlled by valve I31: and the conduit l3 has connected to it conduitsl4, 5, l6, H, and 29 controlled respectively by valves I4a, 5a, 16a, Naand 29a. At the bottom, the regenerator I2 is provided with a conduit 18controlled by valve [8a and connected to a further conduit I9 controlledby valve Ho. The conduit H has an outlet conduit 20 controlled by valve200. and an inlet conduit 2| controlled by valve 2la. Finally, theregenerator I2 is provided in the side thereof with another'conduit 23controlled by a valve 23a having branches 24, and 36 controlledrespectively by valves 24a, 25a and 36a and additional conduits 26, 21and 28 controlled respectively by valves 26a, 21a and 28a are providedin the side of the generator.

Solid fuel such as coke is introduced into the generator I and the plantis operated as follows:

Blow cycle.-The whole or the major part of the air or otheroxygen-containing gas employed is introduced through the conduit 4 andis pre-heated by the heat stored in the ash bed to above the grate 2resulting from a previous operation. In the reaction zone a part of thefuel is burnt and a part of the heat of the blow gases formed remains inthe reaction zone la. The blow gases leave the reaction zone at theaverage temperature thereof and may be used alone or with the additionof secondary air supplied through conduit 6 to pre-heat the fuel lbabove the reaction zone and then leave the generator at a pre-determinedtemperature via conduit 9. The blow gases alone or in admixture withadditional fuel admitted through conduit I6 and if necessary withadditional air or other oxygen-containin gas admitted through conduit I!are used for heating the regenerator I2, and the gases leaving theregenerator by conduit 18 are used for generating steam required for theprocess or for other purposes.

Gas making cycles (a) Down gas making cycle-Steam and/or carbon dioxidealone or in admixture with other gases (according to the propertiesdesired in the gas to be produced) are introduced into the bottom of theregenerator l2 by conduit IE or by a separate conduit (not shown) andare heated therein to a pre-determined temperature. The

gases leave the regenerator l2 by conduit l3 and either alone or inadmixture with steam and/0r water and/or carbon dioxide admitted throughconduit I4 are introduced into the generator I through one or more ofthe conduits 6 (via 29), 1, 8, 9, l0 and II. The gases then pass throughthe reaction zone I a. After leaving the reaction 4 zone a part of thegases produced together with undecomposed steam and/or carbon dioxidemay be removed via conduits 26 and 21, or a part of the heat of thegases produced may be stored in the ash bed lc above the grate 2 and thegases removed via conduits 3, or only a part may be removed via conduits3, the remainder being removed via conduit 4. If a, part of the gases isremoved via conduit 4 it may be cooled if required before reaching thegrate by the injection of water or steam or other gases or oil byconduit 28. The sensible heat of the gases leaving the generator may beused for the generation of steam. If desired part of the gases leavingthe generator may be re-cycled via conduit I9 to the regenerator, theremainder being removed via conduit 20. Additional water and/or steammay be admitted if desired through conduit 2|.

(b) Up gas making cycle-Steam and/ or carbon dioxide is introduced intothe generator I through the conduit 4 and is superheated or preheated bythe heat stored in the ash bed to above the grate 2. The steam and/orcarbon dioxide then passes through the reaction zone la and the productsare removed through one or more of the conduits l, 8, 9, l0 and IIaccording to the properties required in the gas to be produced and thenature of the fuel used. The gases leaving the generator via the conduitl3 are removed via conduit 5.

Referring now to Fig. 2 of the drawings, the apparatus is similar tothat shown in Fig. l but in addition is provided with conduits i5, 30,3|, 32, 33, 34, 35, 31, 38, 39, 40, 46 and 4! controlled respectively byvalves 15a, 30a, 3| a, 32a, 33a, 34a, 35a, 31a, 38a, 39a, 40a, 46a and41a.

Solid fuel such as coke is introduced into the generator I and the plantis operated as follows:

Blow cycle-This is carried out as described above with reference to Fig.1 of the drawings except that water and steam may be introduced into theblow gases through conduit 33 before they enter the regenerator and oilor tar may be introduced into the blow gases leaving the regenerator l2through conduit l8.

Gas making cycles (a) Down gas making cycle.Steam and/or carbon dioxidewith or without one or more of the substances oil, tar or hydrocarbongases (all of which will hereinafter be referred to as oil) (accordingto the properties desired in the gas to be produced) is introduced intothe bottom of the regenerator l2 by the conduit I8 or by a separateconduit (not shown) and is heated therein to a pre-determinedtemperature. The gases leave the regenerator by the conduit I3. Steamand/ or water may be admitted by the conduit i4. Part of the gas leavingthe regenerator may be allowed to leave the system by the conduit 46,oil being introduced if desired through conduit 32, and can be used forheating purposes or subjected to furthcr treatment. The gases in theconduit 13 are then introduced into the generator I via one or more ofthe conduits 6 (via conduit 29), l, 8, 9, l0 and II.

with the gases leaving the generator via the con- Part of the gas fromthe conduit l3" may, however, be sent via conduit 34 to be mixedduits 3as hereinafter described. 011 with or without water or steam is injectedby conduit 33 The gases which enter th generator pass through thereaction zone In. After leaving the reaction zone a part of'the gasesproduced together with undecomposed steam may be removed via conduits 26and 21, and further oil and/or steam or water may be injected viaconduits 38 and 38, or a part of the heat of the gases produced may bestored in the ash bed Ic above the grate 2 and the gases removed viaconduits 3 or only a part may be removed via conduits 3, the remainderbeing removed via conduit 4. It water is added via conduit 33 the gasesin the conduit 23 may be sent to the regenerator for further heating viathe conduit 40. It a part of the gases is removed via'conduit 4 it may bcooled if required before reaching the grate by injection of water orsteam or other gases by a conduit 28 controlled by a valve 280. Thesensible heat of the gases leaving the generator may be used for thegeneration of steam. If desired part of the gases leaving the generatormay be re-cycled via conduit I8 to the regenerator, the remainder beingremoved via conduit 20. Additional water and/or steam may be admitted ifdesired through conduit 2I.

(b) Up gas making cycle.Steam is introduced into the generator I throughthe conduit 4 and is superheated by the heat stored in the ash bed Icabove the grate 2. The steam then passes through th reaction zone Ia.and the products are removed through one or more of the cond-uits 6 (via29), I, 8, 9 and II. The gases leaving via conduits I, 8, and 9 passthrough conduit l3 and if desired may leave the system via conduit 5.Additional oil may be injected through one or more of the conduits 30,3I and 31. Furthermore, steam or water may also be introduced throughconduit 31 and it will be seen that the gases passing through conduit IIreach the regenerator at the bottom thereof via conduit 41. Duringtheir. passage up the regenerator they are further heated and furtheroil may be injected through one or more of theconduits I5, 32 and 33.Instead of removing gases through conduit 43 they may be fed throughconduits I3 and 29 and removed via conduit 6 in which they may be mixedwith gases leaving generator via conduit 6.

Referring now to Fig. 3 of the drawings, the

apparatus is similar to that shown in Fig. l but in addition it isprovided with conduits 4|, 42, 43, 44 and 45 controlled respectively byvalves Ia, 42a, 43a, 44a and 450. e

Solid fuel such as coke is introduced into the generator I and the plantis operated as follows: Biow cycLa-This is carried out as describedabove with reference to Fig. 1 of the drawings except that additionalair may be introduced via conduits 43 and 44 and a part or the whole ofthe blow gases may be removed through one or more :of the conduits 6,I0, I I and 45.

Gas making cycles I (a) Down gas making cycle.steam and/or carbondioxide and/or hydrocarbons alone or in.

erator I2 by the conduit I3 and are introducedinto the generator Ithrough one or more of the conduits I, 3, 9, I and I I The gas is thenpassed through the reaction zone Ia. After leaving the reaction zone thewhole or a part of the gases may be removed through th conduits 26 and21 or a part of the heat of the gases may be stored in the ash bed Icabove the grate 2 and the gases removed via the conduit 4. If desiredpart of the gases leaving the generator may b re-cycled via conduit I3to the regenerator I2, the remainder being removed via conduit 20.Additional water and/or steam may be admitted it desired through conduit2 I.

(b) Up gas making cycle-Steam and/or carbon dioxide and/or hydrocarbonsalone or in admixture with other gases (according ,to the propertiesdesired in the gas to be produced) are introduced into the bottom 01 theregenerator I2 by the conduit I8. The gases leave the regenerator I2 -byconduit 4i, additional water and/or steam and/or carbon dioxide beingintroduced if desired through conduit 42. The gas is then passed throughthe conduits 3into the generator I passing through the reaction zone Iaand leaving via the conduits I, 8, 9 and I3. Alternatively a part or thewhole of the gases may leave the system without passing through thegenerator.

The depth of the reaction zone Ia may be regulated by controlling thepre-heat temperature of the air, the velocity of the blow gases, and byintroducing and removing theair and the gases produced and the blowgases at varying points of the generator.

If oil gas is to be produced itis advantageous to generate producer gasin the generator instead of blue water gas. A part or the whole of theproducer gas may be burnt by means of air or other oxygen-containinggases and the sensible heat of the product may be used directly orindirectly (i. e. using a regenerator and using the regeneratoralternately for heating gases or vapours and using the sensible heat ofthese gases leaving the regenerator for cracking) to crack oil orhydrocarbon gases. Similarly a part or the whole of the water gas may beburnt and used in the same manner if the apparatus is used for makingwater gas instead of producer gas.

More than one regenerator may be used or one regenerator may be dividedinto two parts interconnected by a conduit and valve, in which case bothparts are heated together in one cycle and the two parts used fordifferent purposes in the other cycle. This embodiment of the inventionis described more fully hereinafter with reference to Figs. 10 and 11 ofthe drawings. The gases, etc., may be taken out of or brought intotheregenerator at difl'erent points with predetermined temperatures, forexample by using the conduits 23, 24, 2 5.and 3, and if desiredre-cycled by means of the conduit 35.

Referring to Fig. 4 of the drawings, the generator I is similar to thatshown in Fig. 1 of the drawings, but as will be seen from the drawing isa simplified form of apparatus.

Solid fuel such as coke is introduced into the generator and the plantis operated as follows:

There are no separate blow cycles, and gas is made alternately in thedown and up directions.

(a) Down gas making cycle.0xygen together with steam and/or carbondioxide is introduced through the conduit 9 and the blue water gasproduced leaves through the conduits 3.

(b) Up gas making cgcle.Oxygen and/or steam and/or carbon dioxide isintroduced through conduit 4, and oxygen together with steam and/orcarbon dioxide is introduced through conduits 3, the blue water gasproduced 7 leaving through conduit 9. Ash is removed automaticallythrough the automatic grate 2.

Referring to Fig. of the drawings, this illustrates a somewhat morecomplex form of the generator shown in Fig. 4 of the drawings, and issuitable for the manufacture of carburetted water gas or oil gas.

In addition to the parts shown in Fig. 4 the apparatus also comprisesconduits 53, 54, 55, 56 and 58, controlled respectively by valves 53a,54a, 55a, 56a and 58a, and heat exchanger or boiler 51.

Solid fuels such as coke is introduced into the generator I and theapparatus is operated as follows when manufacturing carburetted watergas.

There is no separate blow cycle and the gas making cycles are effectedas follows:

(a) Down gas making cycle-Oxygen together with steam and/or carbondioxide is introduced through the conduit 9, being pre-heated in theheat exchanger 51, and the gas formed in the reaction zone Ia passesthrough part of the ash bed lo, a part passing through conduits 3, oiland/or tar being injected through the conduits 53 and 54, thecarburetted water gas produced leaving the apparatus through the bottombranch of the conduit; 3. The remainder of the gases produced passesthrough the whole of the ash bed I0 and leaves via the conduit 8.

(b) Up gas making cycle.--0xygen together with steam and/or carbondioxide is introduced through the conduit 58, proceeds through the ashbed la, in which it is heated. A part of the gases produced in thereaction zone Ia leaves via the conduits 6 and II, oil and/or tar beinginjected through the conduits 55 and 58 respectively. The remainder ofthe gases produced leaves through the conduit 9, giving up heat to theboiler or heat exchanger 51.

The apparatus can also be employed for the manufacture of oil gas, inwhich case the generator I is substituted by a gas producer, in whichproducer gas is manufactured instead of water gas, and steam or steamand air is employed instead of oxygen together with steam and/or carbondioxide. In this case a part of the producer gas may be burnt beforeinjecting the oil.

Referring to Fig. 6 of the drawings, this illustrates an apparatusSuitable for the manufacture of synthesis gas and is a modified form ofthe apparatus shown in Fig. 5, in which the heat exchanger 51 is omittedand additional conduits 59, 68, BI, 62, 63, 64, 65 and 66, controlledrespectively by valves 59a, 68a, BIa, 62a, 83a, 64a, 65a and-68a areprovided.

Solid fuel such as coke is introduced into the generator I and the plantis operated as follows:

There is no separate blow period and the gas making cycles are affectedas follows:

(a) Down gas making cucla-Oxygen together with steam and/or carbondioxide is introduced through the conduit 9 and a part of the gasesformed in the reaction zone Ia leaves through the conduits 3,hydrocarbons or hydrocarboncontaining gases and steam and/or carbondioxide being introduced through the conduits 53 and 54 and oxygen withor without steam and/ or carbon dioxide being introduced through theconduits 58 and 88, the synthesis gas leaving through the bottom branchof the conduits 3. The remainder of the gases produced in the reactionzone Ia passes through the ash bed I0 and leaves through the conduit 4.

(b) Up gas making cycle.0xygen with or without steam and/or carbondioxide is intro-- duced through the conduit 88 and a part of the gasesformed in the reaction zone I a leaves through the conduits 6 and II,hydrocarbons or hydrocarbon-containing gases being introduced throughthe conduits 85 and 66 and steam and/or carbon dioxide being introducedthrough the conduits 83 and 84, the products finally leaving through theconduits GI and 62. The remainder of the gases produced in the reactionzone leaves through the conduit 8. Heat exchangers or boilers, or water,steam or gas injection may be used to cool the gases before they reachthe valves. Referring to Fig. 7 of the drawings, this illustrates anapparatus suitable for the manufacture of carburetted water gasconsisting essentially of a generator and two superheaters. Thegenerator resembles in general the generator shown in Fig. 4 of thedrawings, but it has in addition conduits 83 and 54 similar to thoseshown in Figs. 5 and 6 of the drawings and also conduits 81, 88 and 88,controlled respectively by valves 61a, 88a and 88a.

The generator is connected to the first superheater I8 by the conduit'II controlled by valve 'lIa leading from the bottom branch of theconduits 3, the conduit II having a conduit I2 controlled by valve l2aconnected thereto. The superheater 18 is connected to the superheater 18by the conduit 14 controlled by valve 14a, having connected thereto theconduit 15 controlled by valve 15a. An exit conduit 16 controlled byvalve 16a is connected to the bottom of the superheater l3 and are-cycling system is provided by conduit 11 controlled by valve Ila,pump 18 and conduit 19 controlled by valve 19a. In addition, furtherconduits 80, 8i and 82, controlled respectively by valves a, 8Ia and 82aare provided for the introduction of gases as hereinafter described.

Solid fuel such as coke is introduced into the generator I and the plantis operated asfollows:

The steam is introduced through the conduits 89, 88 and 61 into thegenerator I and a part of the gases formed in the reaction zone Iapasses to a part of the ash bed lo and leaves via the conduits 53 and54. The gases leaving the bottom branch of the conduits 3 pass via theconduit II into the superheater 10, oil being introduced through theconduit 12. The gases leaving the superheater 10 pass through conduit14, further oil being introduced through the conduit 15. The gases thenpass into the superheater I3 and leave via conduit 16, further oil beingintroduced through conduit 80. If desired a part of the gases leavingthe superheater 13 may be recirculated thereto via conduits I1, pump 18and conduit 19, further oil being introduced through conduit 8I.Alternatively, the pump 18 may be omitted and the circulation may beeffected by steam injected through conduit 82. If a pump is employed thetemperature of the gases should not be too high at the stage at whichthey pass through the pump.

Referring to Fig. 8 of the drawings, this shows an apparatus suitablefor the manufacture of carburetted water gas comprising a generator,which is similar to that shown in Fig. 4 of the drawings, together witha superheater 18 similar to that shown in Fig. 7 of the drawings. Theapparatus also comprises conduits 83, 84, 88, I8. 81 and 88, controlledrespectively by valves 88a, 84a, 85a, 88a, 81a and 88a.

Solid fuel such as coke is charged into the generator I and the plant isoperated as follows:

Steam and! or carbon dioxide with or without air is introduced into thegenerator I via conduit 9 and a part of the gases produced in thereaction zone Ia passes through a part of the ash bed Ic into theconduits 9, oil being introduced through conduits 63 and 84, thecarburetted water gas thus produced leaving through the bottom branch ofthe conduits 3. The remainder of the gases produced passes through thewhole of the ash bed Ic into the conduit 4, apart leaving through thisconduit and the remainder passing through conduit 88 into thesuperheater I0, leaving via conduit 81, air, oxygen, steam, carbondioxide, oil or tar or a mixture of these being introduced through theconduit 86 and all being introduced through conduit 88. A part of thegas passing through conduit 88 may be led oil through conduit 04, oilbeing introduced through conduit 86.

Referring to Fig. 9 of the drawings, this shows an apparatus suitablefor the manufacture of carburetted water gas comprising a generator anda regenerator divided into two parts. The generator is in generalsimilar to that shown in Fig. l of the drawings, but with modificationsin the conduits connecting the generator with the regenerator. Thus thegenerator I is connected to the lower-part 89 of the regenerator by theconduit 90 controlled by valve 90a, which has branches 9i and 92controlled respectively by valves 9 Ia and 92a connecting the conduit 90with the conduits 8. The generator I is also provided with conduits '93and 94 controlled respectively by valves 93a and 94a, the conduit 94being connected to the conduit 90 by the conduit 96 controlled by valve9Ia, which in turn is connected by the conduit 96 controlled by valve96a to the conduit 83. Conduits 91 controlled by valve 91a and I06controlled by valve I06a connect the top of the generator I with the toppart 98 of the regenerator. In addition, an exit conduit 99 controlledby valve 99a is provided and also inlet conduits I00, IN and I Ibcontrolled respectively by valves I00a, IOIa and IOIc. The upper part 98and the lower part 89 of the regenerator are connected with a conduitI02 controlled by valve I02a, the conduit I02 being connected with theinlet conduit I09 controlled by valve I0la, whilst a further conduit I04controlled by valve I04a is provided at the bottom of the lower part 89of the regenerator, the said conduit I04 having a branch conduit I05controlled by valve I05a for the purpose hereinafter specified.

Solid fuel such as coke is introduced into the generator I and the plantis operated as follows:

Blow cycZe.This is carried out by introducing air via condu ts 3 and 4,thereby heating the reaction zone I a, the blow gases leaving throughconduit 91 and thence proceeding via conduit I06 through the upper part98 of the regenerator, and thence via conduit I02 to the lower part 89of the regenerator, the gases being removed through conduit I04.Additional air is admitted through conduit I M in the first part 01 theregenerator and through I 0Ib in the second part of the regenerator. Theblow gases entering the upper water gas produced leaves through conduits98 and 94 and is carburetted by oil which has been admitted throughconduit I06, pre-heated in the lower part 89 of the regenerator, andthen admitted through conduit 90 and thence through conduits 96 and 96into the conduits 94 and 98 respectively. The remainder of the water gasproduced leaves through conduit 91 and is mixed with gas from theconduit I06, which is produced as follows: Steam is admitted throughconduits I03 and I02 into the upper part 98 of the regenerator in whichit is heated, and oil is admitted through conduit IN and is cracked bythe sensible heat of the steam leaving the upper part 98 of theregenerator. Mixed gases from the conduits 91 and I06 are removed viaconduit 99.

(b) Down gas making cycle-Steam is admitted through conduit I03 andpasses via conduit I02 into the upper part 98 of the regenerator, inwhich it is pre-heated to a temperature of, for example, 1000" C. Thepre-heated steam then passes via conduits I06 and 91 into the top of thegenerator I, water gas being formed in the reaction zone Ia. A part ofthe water gas leaves via conduits 8 and is carburetted in the followingmanner: Oil is passedrthrough conduit I04 into the lower part 89 of theregenerator and the pre-heated oil then passes through conduit 90 and issplit into two streams, a part going through conduit 9i and theremainder through conduit 92. The remainder of the water gas producedleaves through conduit 4.

Referring to Fig. 10 of the drawings, this shows a modification of theapparatus illustrated in Fig. 9 of the drawings, and is also suitablefor the manufacture of carburetted water gas.

The generator and regenerator are in general controlled by valve I08a. Afurtherconduit I09 part 98 of the regenerator may have a temperature of,for example, 1200 C., whilst those entering the lower part 89 of theregenerator may have a temperature of, for example, 450 to 600 C.

Gas making cycles controlled by valve I09a is provided in the top of thelower part of the regenerator, and has two branches, H0 and III,controlled respectively by valves HM and la, which in turn are connectedrespectively to conduits H2 and H3, controlled respectively by valvesII2a and II3a. A manifold I I5 is provided to collect the gases passingthrough conduits H2 and H3 and convey them to the upper part of conduitI02. Conduits I I6 and II! controlled respectively by valves I I61! andI Na in the regenerator part of the system are also provided for thepurpose hereinafter specified.

Solid fuel such as coke is introduced into the generator I and the plantis operated as follows:

Blow cycle.This is carried out by admitting air through conduit I 04,the air being pre-heated in the lower part 89 of the regenerator andpass- 8 via conduits I02, I01 and I I4 into the conduit 4, through whichit is admitted into the generator I. Reaction takes place in thereaction zone Ia and the blow gases leave through conduit 91, additionalpre-lmated air being admitted through conduit I08 from conduit I0'I,whilst still further air is admitted through conduit I00. The blow gasesthen proceed via conduit I06 into the upper part 98 of the regenerator,which is thereby heated, for example to a temperature of 1000 C., thegases leaving the upper part 08 of the regenerator then proceedingthrough conduit I02 to the lower part 80 of the regenerator, which isthereby heated, for example to a temperature of 450 C. The blow gasesthen leave through conduit I04.

Gas making cycles (a) Up gas making cycle.Steam is admitted throughconduit 58 into the generator I and is superheated by passage throughthe ash bed lo, the reaction taking place in the reaction zone Ia. Thewater gas produced leaves via conduits H2 and H3, oil for carburettingbeing injected through conduits H and III, which are supplied withpre-heated oil as follows: 011 is admitted through conduit I and passesthrough the lower part 89 of the regenerator, where it is pre-heated,and thence passes through conduit I09 to conduits H0 and III. The watergas carburetted in conduits I I2 and I I3 leaves via manifold H5 andthence passes to the upper part of conduit I02, through the upper part98 of the regenerator, and leaves through conduit I06. The remainder ofthe water gas leaves through conduit 91 and thence passes through theconduit I06 and the conduit H6, in whch oil is injected through conduitII1. water gas produced, without being carburetted may leave throughconduits 31 and 99.

(b) Down gas making cgcle.Steam is introduced through conduit I03 and issuperheated in the upper part 98 of the regenerator, and thence passesvia conduits I06 and 31 to the top of the generator I. Reaction takesplace in the reaction zone Ia and a part of the water gas producedleaves through conduits 3, oil for carburetting being introduced throughconduits 53 and 54. The remainder of the water gas leaves throughconduit 4. Oil introduced through conduits 53 and 54 may be pre-heatedby passing it through the lower part 80 of the regenerator.

Referring to Fig. 11 of the drawings, this shows an apparatus comprisinga. generator and a regenerator suitable for the manufacture of producergas.

The generator I, in addition to conduits 3 and 4 as used in otherfigures of the drawings, is provid'd with conduits H8 and H3 and I30,controlled respectively by valves I I8a, I I9a and Ia. Conduits H8 andH9 unite in the manifold I2I controlled by valve I2Ia, which is providedwith conduits I22 and I23, controlled respectively by valves I22a and I23a. The manifold I2I is connected to the regenerator I2 by means ofconduit I24, controlled by valve I24a, and the regenerator I2 isprovided at its lower end with a conduit I25, controlled by valve I25a.

Solid fuel such as coke is introduced into the generator I and the plantis operated as follows:

Gas making cycles (a) Down gas making cycle.-Steam and/or air isintroduced into the regenerator I2 through conduit I25 and thenceproceeds through the regenerator I2 to the conduit I24, steam or waterbeing introduced through conduit I23. The mixed gases then proceed tothe manifold I2I, and are introduced into the generator I throughconduits IIB and H9. The producer gas leaves the generator partlythrough conduits 3 and partly through conduit 4.

(b) Up gas making cyclc.-Steam and/or air is introduced into thegenerator I through con If desired, a part of the duit 4, proceedingthrough the ash bed lo, and the producer gas obtained leaves partlythrough conduit I20 and partly through conduits H8 and I I9, from whenceit proceeds via manifold HI and conduit I24 to the regenerator I2, whichis heated thereby, the gas finally leaving through conduit I25.

Referring to Fig. 12 or the drawings, this shows an apparatus somewhatsimilar to that illustrated in Fig. 11 of the drawings, and suitable forthe manufacture of carburetted water gas.

The generator and regenerator are similar to those shownin Fig. 11. Thegenerator I has at the top thereof a conduit I26, controlled by valveI26a, which is connected by the conduit I21, controlled by valve I21a,with the conduit I28, controlled by valve I28a at the top of theregenera-' tor I2. A further conduit I31, controlled by valve I31a, isconnected to the conduit I21 for the purpose hereinafter described. Thebottom branch of the conduits 3 is also connected to the bottom of theregenerator I2 by means of a conduit I29, controlled by valve I29a, saidconduit having a further conduit I30, controlled by valve I 35aconnected thereto. In addition, a, conduit I3I controlled by valve I3Ia,is connected to the conduit I28, whilst conduits H8 and H3 meet at theconduit I32, controlled by valve I32a, which has connected thereto twofurther conduits I33 and I34, controlled respectively by valves H311 andI 34a. A conduit I35, controlled by valve I35a, joins the conduit I32 tothe conduit I36, controlled by valve I36a, which is connected to thebottom of the regenerator.

Solid fuel such as coke is introduced into the generator I and the plantis operated as follows:

Blow cycle.This is carried out by admitting air through conduits 3 and 4into the generator I. The blow gases leave through conduit I23 and passvia conduit I21. Secondary air is introduced through conduit I31, andthe gases then proceed Via conduit I28 into the regenerator I2. The blowgases leave the regenerator I2 through conduit I36.

Gas making cycles (a) Down gas making cgcle.--Steam is admitted throughconduit I26 into the generator I, water gas being formed in the reactionzone Ia. Part of the water gas formed leaves via conduit 4 and theremainder leaves through conduits 3, tar and/or oil being injectedthrough conduits 53 and 54 to carburet thewater gas. The gases leavingthe bottom branch of the conduits 3 proceed via the conduit I29 toconduit I36, steam and/0r water being injected through conduit I30. Thecarburetted water gas then proceeds to the regenerator I2 in which it isfurther heated and additional oil is introduced through conduit I3I. Ifdesired, a part of the gases produced can be re-cycled to the generatorI via conduits I21 and I26.

b) Up gas making cycle.-Steam is introduced through conduit 58 into thegenerator I and the water gas produced in the reaction zone Ia leavesthrough conduits H8 and H0 and then proceeds via conduit I32, additionaltar and/or oil being injected through conduit I33 and water and/or steamthrough conduit I34. The carburetted gas then proceeds via conduit I35and conduit I36 to the regenerator I2 where it is further heated, andleaves via conduit I28, further oil being injected through conduit I3I.

Referring to Fig. 13 of the drawings, this shows an apparatus comprisinga generator and two synthesis gas from coal and residual gas or theFischer-Tropsch and similar syntheses.

In addition to the-generator I, the apparatus comprises the regeneratorsI38 and I39 which are connected together by the conduit I40, controlledby valves "01: and I40d, and the 'regenerator. I39 is provided with anoutlet conduit I40b controlled by valve I40c. The conduit I40 hasconnected to it conduits I4I, I42, I43, -,I44, I45, I48 and I41,controlled respectively by valves I4Ia, M, 30, MM, I45a, I46a and I41a.The regenerator I38 has connected to the bottom thereof a conduit I48,controlled by valve I48a, passingthrough a heat exchanger I49 and havingconnected to it conduit I50, controlled by valve I50a. Conduit I48 isalso connected to a conduit II, controlled by valve I5Ia, which in turnis connected by the conduit I62, controlled by valve I52a, with theconduit I40. The conduit IY 5I also has connected thereto conduits I53.I54 and I55. controlled respectively by valves I53a, I640. and I55a. Theconduit I40 is also connected to the regenerator I39 by conduit I56,controlled by valve ma. A conduit I59, controlled by valve IBM. is alsonrn'ddcrl which oins the conduits 3 with a conduit I60, controlled byvalve I60a, connected to the bottom of the regenerator I39. The conduitI 60 also has connected thereto conduits I8I and I62, controlledrespectively by valves I6Ia and I62a. The generator I has connectedthereto conduits I63, I64. I65 and I66,

controlled respectively by valves I63a, I84a, Ilia and I66a. The conduitI85 has connected thereto conduits I61 and I68, controlled respective byal es "We and IBM. whilst the conduit I66 has connected thereto conduitsI69 and I10 controlled respectively by, valves I69a and 11011. Theconduits I65 and I66 meet and are joined to the conduit I1I, controll dby valve I1I a, which is connected to the conduit I40. The generator isalso provided at the top thereof with a conduit I12 controlled by valveI12a. connectin it with the conduit I; The conduit I40 also has abranchconduit I13, controlled by valve "311.

Coal is introduced into the generator I and the plant is o erated asfollows:

First blow cycle.-Air is admitted to the generator I through conduit 4,secondary air beine admitted through conduits I63 and I64 01 I61 andI69. Steam which may be super-heated or other gases may be admittedthrough conduits I63 and I64 and a part of the blow gases producedleaves the generator I through conduits I65 and I86, and reaches theconduit I40 via conduit I1I, liquid or gaseous fuel being introducedthrough conduits I68 and I10. The remainder of the blow gases leaves theenerator I via conduit I12 and thus alsoreaches the conduit I40. Thegases in the conduit I40 pass into the regenerator I39,-

through conduit I 6| into the regenerator. I39.

The steam' leaves the regenerator: I39 throu h conduit I40 and passesthrough conduits I1 I, I65 and I66 into the fuel bed Ib. A part of thesteam passes into the reaction zone Ia wherein water gas is made, andthe other part passes through the'fuel bed Ib, carbonises the coal andleaves through conduits I10 and I88 and thence may pass either into theregenerator I38 via conduit I40 or is sent for purification via conduitsI40, I52 and lil. At thesame time stwm, residual gas and carbonisationgas are admitted through conduit I13 into the regenerator IR. Theproducts leave through conduit I48 and are sent to the synthesis plantvia conduit I53. If desired, a part or the whole of the steam may leavethe regenerator I39 through conduit I68.

superheated steam may be admitted through conduit I44 in which case theregenerator I39 may be used for other purposes such as decomposition ofresidual gases or carbonisation gases admitted through conduit I62.

Up gas makinq cycle.-Steam is admitted through conduit 4 into thegenerator I, a part of the gas produced leaving through conduits I andI66. Additional steam which may be superheated is admitted throughconduits I61 and I68, the gas then'proc'eeding through conduit HI intoconduit I40. The remainder of the gas produced in the generatorleavesthrou h conduit I12 and thence passes into conduit M0. The gas inconduit I40 is either sent to the rei enerator I38 or is removed for coling and urification via conduits I52 and I5I. If desired. water and/orsteam and/or carbon dioxide is admitted through conduit I43. residualgas being admitted through conduit I42 and steam being admitted throu hconduit MI.

The gases leave the regenerator I38 through conduit I48, passing throughheat exchan er I49. At the same time the regenerator I39 is heated byburning additional gaseous or liquid fuel introduced through conduitl46by means of air introduced through conduit I41 Second blo1oc1/cle.-Resdua1 gas is admitted through conduit I6I and steam throu h conduit I62into the regenerat r I39. The decomposed gas leaving the regenerator I39passes via conaction zone Ia. and a part leaves the enerator throughconduits"l65 and I66, the remainder leaving through conduit I12,bothparts then I being sent to the regenerator I38 throu h confuel trough conduit I54 and air throu h con-- duits I40, I52, I5I and I48 aftr admission of may be sup rh at d may be admitted through conduits I63and I64.

Referrin to Fi 14 of the drawings, this shows an apparatus consisting ofa generator and two ree'enerators, which maybe regarded as asimplifiedform of theapparatus shown in Fig. 13,

" and can also be used for the manufactureof synthesis gas. Y a I Thgenerator I-has conduits which a're'referred to in previous figures ofthe drawings, and

is connected to t e regenerator I38 byth'e conduits I15 and I81,controlled respectively by valves H511 and I81a, and to the regeneratorI39 by the conduits I16 and I 80,. controlled re-' spec'tively by valvesI16a and Ia. Theconduit I15 continues'as conduit I86,'-'contr0lled byvalve I88a, and the conduit I81 has'conneeted T to it two furtherconduits I88 and I89, controlled respectively by valves I88a and I 89a.Likewise, the conduit I80 has connected to it conduits I19 and I8I,controlled respectively by valves I19aand I8Ia,'. whilst the conduit I18has connected to it the conduit I11, controlled by valve I11a. Theconduit I58, controlled by v'alveI58a,

connects the conduits I and I48.-' The conduit I58 has connected thereto,conduits I92and I93,

connected to it the conduit I 83, controlled by valve I83a, and theconduit I84, controlled by valve I84a.

Solid fuel such as coke is introduced into the generator I and the plantis operated as follows:

First blow cycle-Air, which may be pre-hc'at-- ed, is introduced throughconduit 4 into" the generator I, and secondary air is introduced throughconduits I03 and I64. The blow gases leave the generator I by theconduit 9 and proceed through conduits I15 and I80 into the regeneratorI39, additional fuel being introduced through conduit I18 and additionalair through conduit I8I. The blow gases leave the regenerator I39 by theconduit I82. Steam and/or carbon dioxide is admitted through conduitI80- and residual gas and/or other hydrocarbon-containing fuel isadmitted through conduit I9I, the mixture proceeding through conduit I48into the regenerator I 38, the gases leaving by the conduit I81. Thegases are then removed through conduit I85.

Down gas making cycZe.Steam and/or carbon dioxide, with or withoutresidual gas, is admitted through conduits I 83 and I84 into theregenerator I39, and the gases leave through conduit I80. Further steamand/or carbon dioxide is admitted through conduit I18 and water and/orsteam and/or carbon dioxide through conduit I11, whilst superheatedsteam or preheated carbon dioxide is admitted through conduit I14, andthe gas mixture then proceeds via conduit 9 into the top of thegenerator I, a part of the gases produced leaving through conduit 4 andthe remainder leaving through conduits 3. Steam and/or carbon dioxide isalso admitted through conduit I90 and residual gas through conduit. I9Iinto the regenerator I38, and the gases produced leave through conduitI88.

Up gas making cycle-Steam is admitted through conduit 58 into thegenerator I and the water gas produced is removed through conduits 9 andI51. Fuel is admitted through conduit I18 and air through conduit I8I,the gases leaving the regenerator I39 through conduit I82. Steam and/orcarbon dioxide is also admitted through conduit I86 and residual gasthrough conduit I89 into the regenerator I38, the gases leaving theregenerator I38 through conduit I48.

Second blow cycIe.--Air is admitted through conduit 4 into the generatorI, secondary air being admitted through conduits I83 and I84. The blowgases leave through conduit 9 and are sent through conduits I15 and I58to the regenerator I88, air being admitted through conduit I93 andadditional fuel through conduit I92. The gases leave the regenerator I38through conduit I81. Steam and/or carbon dioxide is also admitted andNz=3.5

. 1s through conduit I83 conduit 'I84 into the regenerator I39, thegases produced leaving through conduit I18.

some examples of the use of the apparatus ac cording 'tothe inventionwill now be given.

1. Manufacture of blue water gas The apparatus shown in Fig. 1 of thedrawings was used blowing. periods being employed.

The fuel used was coke, which had an average analysis of C=96.'7%,H2=0;4%, -O:= 0.4%,

S=1.2% and Nz=1.3% (calculated on a dry ash free basis) and itscalorific value calculated on the same basis was 8000 Cals. The -gasproduction per gas making period was 500 cubic metres (calculated on adry basis at 0 C. and 760 mms..

pressure); the average temperature in the reaction zone was 1100" C. andthe average temperature of the gases and undecomposed steam leaving thereaction zone was also 1100 C. The

composition of the blue water gas" produced was CO=42.8%, CO2=4.0%,Ha=49.3%, CH4=0.4% The composition of the 'blow gases leaving thegenerator was C02=16.0%, CO=8.0%, and N2=76.0%, and the air required percubic metre of blow gas was 0.96 cubic metre.

The heat (R) required for the chemical reaction (taking into account thecomposition of the gas generated and the composition of the fuel used)in the production of the blue water gas as described above is 490 Cals.per cubic metre of blue water gas produced, and is calculated from thefollowing formula:

reo=heat of formation of carbon monoxide in Cals.

Tco =heat of formation of carbon dioxide in Cals.

C0, C02 and CH4 =the concentrations of carbon monoxide, carbon dioxideand methane in the gas, respectively.

Nc+=concentration of nitrogenin the gas.

Ne=concentration of nitrogen in the fuel.

ing cycle using 101 kgms. of steam. Blowingup I effected in the updirection.

Down gas making cycle-The sensible heat of the gases produced and.undecomposed steam leaving the reaction zone Ia was 126,000 Cals. Thesensible heat of the gases leaving through the conduits 3 was 16,300Cals. and the sensible heat of the gases leaving through conduit 4 was10,700 Ca1s., making a total of 27,000 Cals.

and residuahgas through 17 the gases leaving the reaction zone la is84,000 Cals.

The sensible heat of the gases leaving the generator l'is 29,000 Cals.so that the heat stored in the fuel bed lb is 55,000 Cals.

The heat removed from the ash bed lc by the steam, assuming that thesteam enters the reaction zone la at 1050 C. is ll l050X0.513 101x1200.447=54,400-5,400=49,000 Cals. The sensible heat of the gases andundecomposed steam leaving the reaction zone or is 126,000+ 84,000-.210.000 Cals. per cycle. The heat required for the reaction is 500490=245,000 Cals.

vThe heat required for the production of 500 cubic metres of blue watergas, without taking into account the heat introduced by the coke andsteam into the reaction zone is 210,000+ 245,000=455,000 Cals. 'percycle. The heat brought into the reaction zone by the coke (assumingthat the-coke contains 87.0% of carbon and that the amount of coke usedin the gas making cycle is 0.290 kgm. per cubic metre and 0.155 kgm. percubic metre in the blow cycle), the coke entering the reaction zone at1090 C., is: Gas making cycle, 0.290X500X1090X0.377= 60,000 Cals. Blowcycle, 0.155x500X1090X 0.377=32,000 Cals.

The heat brought into the reaction zone by the steam is81,000+54,000=135,000' Cals., so that the total heat brought into thereaction zone by the steam and the coke in the gas making cycle is195,000 Cals. The heat to be stored by the blow gases in the reactionzone per cycle is 455,000195,000=260,000 Cals.

The amount of blow gases required to store 260,000 Cals. per cycle iscalculated as follows: The temperature of the blow gases leaving thereaction zone is 1100 C. and the heat introduced by 1 cubic metre ofblow gases is 0.16X 4364+0.08 1344=807, to which must be added the heatwhich is generated from the hydrogen and sulphur present in the coke,which amounts to 19 Cals. (after deducting the heat in the gases leavingthe reaction zone), so that the total heat generated by 1 cubic metre ofblow gases is 826 Cals. As the gases leave the reaction zone at 1100 C.the heat stored in the reaction zone per cubic metre of blow gasesobtained from 0.96 cubic metre of air and 0.151 kgm. of coke is 826-11000.360=420 Cals. per cubic metre of blow gases. The total heat to beintroduced with the blow gases, taking into account the heat introducedwith the coke in the blow cycle and the heat introduced with the air is260,000- (32,000+48,000) =180,000 Cals. Therefore the amount of blowgases required per cycle is 430 cubic metres and the amount of airrequired 412 cubic metres per cycle.

The carbon required in the blow cycle to generate 1 cubic metre of bluewater gas is The output or capacity of the apparatus is very high, asonly 520 Cals. require to be stored per cubic metre of gas to bemanufactured. The

18 velocities of the gases are high and the temperature drop in thereaction zone is not very rapid.

In the above calculations, the sensible heat of the air entering thegenerator at a temperature of 20 C. and the sensible heat of the ashleaving the generator at a temperature of C. has been ignored.

The heat'stored in the apparatus at various parts is as follows: In thedown gas making cycle, the steam removed from the fuel 73,000 Cals. and99,000 Cals. is stored in the ash bed, whilst in the up gas makingcycle. 49,000 Cals. is removed from the ash bed by the steam and 55,000Cals. is stored in the fuel bed. In the blow cycle, 48,000 Cals. isremoved from the ash bed by the air, whilst 110,000 Cals. is stored inthe fuel bed.

Assuming that the cross-sectional area of the generator is 10 squaremetres and that the fuel bed outside the reaction zone is equivalent toa height of 1 metre, the amount of coke in this part of the bed will be6,000 kgms., and to store, as in this case, 165,000 Cals. an increase oftemperature of 75 C. is required.

In the ash bed, to store 99,000 Cals., assuming the same volume and theweight of the ash to be 900 kgms., an increase of temperature of 42 C.is required.

If the volume of the fuel and the ash is doubled, the temperatureincrease or decrease per cycle will b 375 C. and 21 C.

The storage of heat in the fuel and the ash can also be varied and atthe same time the temperature of the gases used may be changed byvarying the amount of gas in the down and up directions.

Thus, for example, if the generator I is in operation and thetemperature at the points where the upper branches of the conduits 3enter the generator is too high, the temperature may be lowered byincreasing the thickness of the ash bed to and more heat is' thus storedin the ash, and the gas arriveswith a lower temperature at this point,and in the next up cycle and blow cycle more heat is taken from the ashbed. Should the temperature at the point where the conduit.4 enters thegenerator I be too high, more gases may be taken out via conduits 3 andthe temperature at the point where the conduit 4 enters the generatormay thus be lowered.

The same considerations apply to the regulation of the temperatureoutside the reaction zone la in the upper part of the generator, andthis may be regulated by increasing or decreasing the thickness of thefuel bed and by taking out various amountsof the gases via the conduits9 and 6.

The temperature of the gases entering or leaving the conduit 4 may alsobe regulated by the injection of water and steam or gases.

The variation in the depth and temperature of the reaction zone iseffected by changing the temperature and velocity of the air enteringthe reaction zone.

2. Manufacture of carburetted water gas for carburetting by utilisingthe sensible heat of g the gases produced can be found by using asimplifled formula which I have developed, based on results obtained inthis method of cracking of gas oil and which takes into account 1) Thesensible heat required to bring the gases obtained and leaving thecracking zone to the temperature of the cracking reaction, (2) Thereaction heat which is the diflerence between the heat in the oil andhydrogen consumed in the cracking and the products leaving the reactionzone, and (3) The losses:

s.-s, (ti-Z) (0.0004t+0.310)

S1=Sensible heat of the gases entering the cracking zone;

S2=Sensible heat of the gases leaving the cracking zone at thetemperature t;

t=Temperature at which the cracking is accomplished;

a:=A factor which will vary according to the conditions of the crackingand the yield of the products obtained in the cracking and which may becalculated using the following formula:

" o.ooo4:+o.31o

Or if the oil is pre-heated and the pre-heat temperature is t1 theformula is:

If a regenerator is used for water gas production from tar or the likethere must be taken into account the fact that the reaction heat of thewater gas production is negative and must be provided by the heat storedin the checker bricks or by the combustion of oxygen and part of thefuel used. The hydrogen content of the fuel must also be taken intoaccount as the hydrogen does not require reaction heat and steam. As thecalorific value of the gas obtained may be considerably varied by theamount of steam or carbon dioxide used, it is necessary for the dimengkgs. oil= wherein sions of the conduits to be sumciently large to havethe required flexibility.

Part of the gases may be removed at different points and in severalstreams from the regenerator, and to obtain gases with differentcalorific values and difierent compositions conduits should be providedfor this purpose.

The composition of the gases taken out at these conduits may beregulated, in addition to the above-mentioned ways, by the variation of=the temperature of the reaction and the points of the regenerator atwhich the gases are bled off.

3. Production of synthesis gas and synthesis products from coal andresidual gas (see Fig. 13 of the drawings) produce a cubic metre of thiswater gas can be calculated as follows:

Down gas making cycle.The gases leaving the reaction zone consist of 525cubic metres of water gas and 52.5 kgms. of steam. and the sensible heatof the gases leaving the reaction zone at a 20 temperature of 1100 C. is525x1100x0.33+525x 1100 0.5l7=221,000 Cals. The sensible heat in the 300cubic metres of water gas and 30 kgms. of steam leaving the generatorthrough conduits 3 at 500 C. is 300X500X0.31'1+30 500 0.4'1= 55.000Cals.

The sensibleheat in the 225 cubic metres of water gas and 22.5 kgms. ofsteam leaving the generator through conduit 4 at 200 C. is 225X200X0.312+22.5x200x0.450=16,000 Cals., so that the total heat removedwith the gases from the generator is 71,000 Cals.

The heat stored in the ash bed is 150,000 Cals. The sensible heat of 235kgms. of steam entering the generator, from the regenerate: at 650 C. is235X650 0.485=74,000 Cals. The sensible heat removed from theregenerator with the steam is 235x650 0.485285x 120 0.44=81,000 Cals.

The sensible heat in the steam entering the reaction zone of thegenerator at 1000 C. is 235x 1000 0.510=120,000 Cals.

The heat removed from the fuel bed by the steam is 120,000'I4,000=46,000Cals.

Up gas making cycle.-The gas leaving the reaction zone in the up gasmaking cycle consists of 225 cubic metres of water gas and 22.5 kgms. ofsteam. The sensible heat of the gases leaving the reaction zone at 1100C. is: 225XlX 0.33+22.5 1100x0.517=95,000 Cals.. The sensible heat ofthe gases leaving the generator at 500 C. is 225x500 X0.317+22.5500x0.470= 41,000 Cals.

The heat transmitted to the fuel bed by the gases leaving the generatorin the up gas making cycle is 95,000-41,000=54,000 Cals.

The heat removed from the ash bed by the steam entering the reactionzone at 1050 C. is 100=1050 0.513-100 120x0.44'7=49,000 Cals.

0.432 kgm. of coke were used for the production of one cubic metre ofgas and the coke directly converted into water gas was 0.280 kgm. percubic metre of gas. 0.150 kgm. of coke is used in the blow period percubic metre of gas produced and consequently the heat brought into thereaction zone in the gas making period and blow cycle at a temperatureof 1050 C. will be 0.280X1050X 0.37x50+0.152 1050 0.37 50=125,000 Cals.

The blow gases leave the generator at 400 C. and the heat stored by theblow gases in the fuel bed is 610x1100 0.3'7610 470 0.32=1'71,000 Cals.

The heat required to be stored in the reaction zone per cycle withouttaking into account the heat introduced by the coke and steam but takinginto account the heat of formation of the water gas, i. e. 460 Cals. percubic metre, is 221,000+ 95,000+750x460=661,000 Cals. per cycle.

The heat required to be stored in the reaction zone taking into accountthe heat introduced with the steam and coke in the gas making cycle is661,000 (120,000+54,000+81,000) 406,000 Cals., or 541 Cals. per cubicmetre of water gas produced.

The heat required to be introduced with the blow gases taking intoaccount the heat introduced by the air and coke used in the blow cycleis 406,000 [44,000+ (150,000-49,000) ]=256,000 Cals.

The amount of blow gases required per cycle can be calculated asdescribed above in Example 1 in connection with the production of bluewater gas, and amount to 610 cubic metres. The amount of air requiredper cycle is 610X0.96=585 cubic metres. The air is pre-heated in the ashbed to 540 C. The coke required per cubic metre assume 21 of gas, takinginto account a loss of 7.0% is 1.07x0.403=0.43 kgm. per cubic metre.

Using 405 kgms. of coal per cycle from which is obtained 750 cubicmetres of water gas of the composition referred to above, there areobtained 133 cubic metresof carbonisation gases which afterdecomposition in the regenerator give 240 cubic metres'of gas having thefollowing composition: CO=27.0%, H2='l0.0%, CH4=1.0% and Cz+Nz=2.0%,together with 10.1 kgms. of tar, from which after-decomposition 40 cubicmetres are obtained having the following composition: CO=40.0%,H2=5'7.0%, CH4=1.0% and Thus, from the 405 kgms. of coal, 1060 cubicmetres of gas are obtained having the following composition: CO=38.0%,Hz=57.5%, CH4=1.0% and CO2+N2=3.5%.

This gas can be used as such for the Fischer- Tropsch or similarsynthesis (for instance for production of olefine-rich products) orafter adjusting the ration of COzH to 1:2, a gas of the followingcomposition is obtained: CO=32.0%, Hz=63.5%, CH4=1.0% and CO2+N2=3.5%.

Assuming a contraction of 60% in the synthesis oven and a yield of 106gms. of liquid and hydrocarbon gases containing three and four carbonatoms in the molecule per cubic metre of synthesis gas, the compositionof the residual gas will be: CO=30.0%, H2"=5l.0%, CH4=10.0% andCO2+N2=9.0%. From this gas decomposed in the regenerators (as shown anddescribed in Fig. 14) 1.27 cubic metres of decomposed gas can beobtained per cubic metre of residual gas, having the followingcomposition: CO=30.7%, Hz=6l.5%, CH4=0.8% and CO2+N2=7.0%. A part ofthis residual gas is mixed with the water gas and a part is taken outand treated separately so as not unduly to enrich the synthesis withcarbon dioxide, nitrogen and the like.

The total amount of water gas and decomposed residual gas is 1520 cubicmetres per cycle, and after being subjected to the synthesis Process acontraction of 60% is obtained, so that 608 cubic metres of residual gasare obtained which after decomposition give 770 cubic metres of gas, ofwhich 460 cubic metres are mixed with 1060 metres of water gas and 310cubic metres are treated separately, the amount of synthesis productsobtained being 194 kgms. per 405 kgms. of coal, so that the amount ofcoal required per kgm. of synthesis products is 2.08 kgms.

For the heat required in the regenerators and, if desired, for steamgeneration, the following sources are available:

(1) The sensible heat in the blow gases leaving the regenerators havingan average temperature of 400 0.;

(2) The chemical or potential heat in the blow gases containing 8% ofcarbon monoxide;

(3) The heat in the residual gases which are obtainable from thesynthesis gas which treated separately;

(4) The sensible heat of the decomposed gases leaving the regenerator,which can be used if required, in heat exchangers or boilers to preheatthe gases or steam required for the processes or to generate steam.

It has been found that these amounts are sufficient for the operation ofthe apparatus and it has further been found that by using this apparatusand using a coal having a calorific value of 7600 Cals. per kgm., 63.0%of the calorific value of the coal is converted into hydrocarbon liquidsand hydrocarbon gases containing three and four carbon atoms in themolecule, and the output or the capacity of the apparatus is very high.

Other fuels such as coke, anthracite, lignite or peat may be usedadvantageously, and gases of other compositions, such as thosecontaining a ratio of 00:11: of between 1:1 and 2:1 (using carbondioxide instead of steam) may be advantageously produced.

Even if the yield per cubic metre is lower practically the same resultsare obtainable but the dimensions of the plant and the conduits must bechosen accordingly, and the above method of calculation assistsin'designing the plant;

The average inert content and composition of the synthesis gases is 6%of carbon dioxide plus nitrogen, and the composition of the synthesisgas is: CO=31.0%, Hz=62.0%, CH4=1.0% and CO2+N2=6-0%. I

The composition of the gas treated separately is: C0=30.7%, H2=61.5%,CH4=0.8% and CO2+N==7.0%.

In all the embodiments described above the blow cycle may be carried outin the up and down directions, if desired.

The operation of "purging may be introduced where required in any of theembodiments referred to above.

I claim:

1. An intermittent process for the manufacture of water gas in agenerator operated to produce an ash bed resting on a grate in thebottom thereof, a reaction zone above the ash bed, formed by blastingthe fuel to incandescence, and a fuel bed above the reaction zone,comprising the steps of blasting fuel in said reaction zone toincandescence by means of a blast of air passing in an up directionsuccessively through said grate and said ash bed hot from a previousoperation, passing the hot blast gases leaving the top of said reactionzone to a regenerator to heat the same, then initiating the gas makingcycle by passing steam through the heated regenerator and thencedownwardly through the reaction zone to produce water gas, passing thewater gas from said reaction zone downwardly into the ash bed andremoving said water gas through an outlet in the generator wall which islocated at a fixed point above the grate, regulating the depth of theash bed between the point of withdrawal of the water gas and the bottomof the reaction zone so as to store therein a large part of the sensibleheat of the water gas passing therethrough, and utilizing the thusextracted heat from the water gas made in said gas making down run topreheat gases led to said generator through said ash bed in a succeedingup run.

2. A process according to claim 1 wherein a part of the water gas andundecomposed steam passing downwardly into the ash zone is removedthrough said fixed gas outlet and the remainder from below the grate andregulating the proportions of water gas removed from above and below thegrate so as to prevent the temperature of the ash bed just above thegrate from rising above 450 F. v

3. An intermittent process for the manufacture of carburetted water gasin a generator operated to produce an ash bed resting on a grate in thebottom thereof, a, reaction zone above the ash bed, formed by blastingthe fuel to incandescence, and a fuel bed above the reaction zone,comprising the steps of blasting fuel in said reaction zone toincandescence by means of a blast of air passing in an up directionsuccessively through said grate and said ash bed hot from a 23 previousoperation, passing the hot blast gases leaving the top of said reactionzone to a regenerator to heat the same, then initiating the gas makingcycle by passing steam through the heated regenerator and thencedownwardly through the reaction zone to produce water gas, passing thewater gas from said reaction zone downwardly into the ash bed andremoving said water gas through an outlet in the generator wall which islocated at a fixed point above the grate, regulating the depth of theash bed between the point of withdrawal of the water gas and the bottomof the reaction zone so as to store therein a part of the sensible heatof the water gas passing therethrough, utilizing the thus extracted heatfrom the water gas made in said gas making down run to preheat gases ledto said generator through said ash bed in a succeeding up run, andinjecting a hydrocarbon into 1 24 the so produced water gas after itleaves the generator to carburet said water gas.

mom STEINSCHLAEGER.

REFERENCES CITED The following references are of record in the file ofthis patent:

UNITED STATES PATENTS 10 Number Name Date 858,589 Eyermann July 2, 19071,085,806 Evans Feb. 3, 1914 1,573,524 Rose Feb. 16, 1926 1,752,036Steere Mar. 25, 1930 FOREIGN PATENTS Number Country Date 36,715Switzerland Apr. 3, 1906 328,642 Great Britain Apr. 25, 1930 345,411Great Britain Mar. 26, 1931

